Novel enzymatic phase transfer solvent for co2/h2s capture

ABSTRACT

The present invention relates to a novel phase transfer solvent composition for enhanced CO2 and/or H2S capture from flue gas and biogas having various gaseous compositions. Further, the present invention provides a process of preparing the phase transfer solvent composition of the present invention.

TECHNICAL FIELD

The present disclosure relates generally to the field of Environmental Sciences and Technology. In particular, the present invention relates to a novel phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions. More specifically, the disclosure relates to improved enzymatic and solvent systems, which upon CO₂/H₂S capture forms selective phases with higher CO₂/H₂S loading efficiency and low regeneration energy over the existing solvent systems.

BACKGROUND ART

CO₂ emission from post-combustion streams is the major anthropogenic source of greenhouse gas responsible for global climate change. With the ever-growing industrial demand of fossil fuel use, CO₂ accumulation within the atmosphere is predicted to increase substantially. To reduce the impact of the CO₂ emissions from multiple sources, capture of CO₂ has been advocated.

Among the post combustion carbon capture technologies, chemical absorption using aqueous amine solutions with thermal regeneration of the solvent is the most developed and applied technology for CO₂ capture. Most of the energy required for CO₂capture in amine scrubbing systems is used for regenerating the solvent, which makes the amine scrubbing very cost intensive for their commercial application. The development of new solvents or solvent blends is an important way of reducing the energy demand in amine scrubbing plants.

New class of solvent systems known as phase transitional solvents (PTS), have attracted increased interest for their potential to substantially reduce both energy use and equipment costs for CO₂ capture. These solvents are homogeneous (single-phase) solvents before CO₂ is loaded and upon CO₂ absorption or a temperature shift, they form multiple phases:

a CO₂-enriched phase and a CO₂-lean phase. Because only the CO₂-enriched liquid phase is used for solvent regeneration, the mass of solvent that requires regeneration is decreased. Consequently, the heat required to heat the solvent (sensible heat) is reduced.

There are few CO₂ absorption and desorption using phase transfer solvent have been disclosed in the prior art.

US20070237695A1 relates to a method and system for gas separation using a liquid absorbent absorbing one of the gases to be separated, where the absorbent spontaneously separates into a phase rich in the absorbed gas, and a phase lean in the absorbed gas. The active agent in the not identified but preferred agents is indicated to be selected from the group consisting of alkaline salts, ammonium, alkanolamines, amines, amides and combinations thereof.

WO2013000953A2 described a liquid, aqueous CO₂ absorbent comprising two or more amine compounds, where the aqueous solution of amines having absorbed CO₂ is not, or only partly miscible with an aqueous solution of amines not having absorbed CO₂, where at least one of the amines is a tertiary amine, and where at least one of the amines is a primary and/or a secondary amine, wherein the tertiary amine is DEEA and the primary and/or secondary amine(s) is (are) selected from DAB, DAP, DiAP, DMPDA, HEP, or the tertiary amine is DIPAE, or N-TBDEA and primary and/or secondary amine(s) is (are) selected from DAB, DAP, DiAP, DMPDA, HEP, MAPA, and MEA, and a method for CO₂ capture using the CO₂ absorbent.

WO2010126694A1relates to a method for de-acidizing an acid gas mixture using an absorbent comprising an amine dissolved in a mixture at a first concentration. After absorption of the acid gas, the absorbent forms a concentrated-amine phase, this is separated from the remainder of the absorbent and is introduced into a regeneration unit, whereas the remaining of the absorbent is recycled back into the absorption unit. A series of organic solvents are mentioned as the solvent, together with water and aqueous solutions. Organic solvents are mentioned as preferred solvents. The only exemplified absorbents are MEA in isooctane, which spontaneously forms a concentrated amine phase containing MEA and the reaction product of MEA and CO₂, and an aqueous carbonate solution, which forms insoluble bicarbonate on absorption of CO₂.

WO2010044836A1 relates to a method for de-acidizing an acid gas mixture using an absorbent comprising a carrier phase and an organic phase that is immiscible with the carrier phase. Introduction of an organic solvent as described herein is unwanted, mixed solvent systems add complexity to the systems.

WO2017035667A1 The present description relates to recombinant or engineered carbonic anhydrase polypeptides, variants, and functional derivatives thereof, having improved properties that make them advantageous for use in CO₂ capture operations (e.g., CO₂ capture solvents, alkaline pH, and/or elevated temperatures), as well as polynucleotides and vectors encoding same. The present description also relates to methods, processes and systems for CO₂capture which make use of the recombinant or engineered carbonic anhydrase polypeptides, variants, and functional derivatives thereof.

CA2827024A1 describes a carbonic anhydrase system and processes are disclosed. The system has a reaction chamber, liquid inlet, gas inlet, liquid outlet and gas outlet, and uses carbonic anhydrase on or in substrates in suspension in the liquid for catalyzing a reaction of CO₂ into bicarbonate and hydrogen ions to obtain a treated gas and an ion-rich solution.

Ye et. al “Novel biphasic solvent with tunable phase separation for CO₂ capture: Role of water content in mechanism, kinetics, and energy penalty.” Environmental science & technology 53, no. 8 (2019): 4470-4479 describes a phase transfer system composed of triethylenetetramine (TETA) and 2-(diethylamino) ethanol (DEEA) blends.

Pinto et.al “Evaluation of a phase change solvent for CO₂ capture: Absorption and desorption tests.” International Journal of Greenhouse Gas Control 28 (2014): 318-327 describes a blend of a tertiary amine (DEEA) and a diamine (MAPA) for CO₂ capture.

Jiang et.al, Environmental Science & Technology 54, no. 12 (2020): 7601-7610 describes a phase splitting agent-regulated biphasic solvent for efficient CO₂ capture with a low heat duty.

The drawbacks of the above-said process are:

-   -   Low CO₂ loading capacity and high desorption energy.     -   Low cyclic capacity during subsequent absorption and desorption         cycles.     -   Described prior art has provision for removal CO₂ and not         suitable for H₂S removal.     -   Simultaneous CO₂ and H₂S removal essential for various processes         including biogas purification.     -   Selective phase formation for CO₂ and H₂S is not possible.     -   Sluggish kinetics for CO₂/H₂S capture.     -   Longer time for phase formation.     -   High concentration amine solution required.     -   Higher amine degradation.     -   Higher circulation rates are required for removal of CO₂ to         desired levels.

The present address the problem existing in the art by providing a novel phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions. More specifically, the disclosure relates to improved enzymatic and solvent systems, which upon CO₂/H₂S capture forms selective phases with higher CO₂/H₂S loading efficiency and low regeneration energy over the existing solvent systems. The disclosure further provides a phase transfer solvent composed of a primary amine/secondary amine, a tertiary amine, a hyperthermophilic enzyme, thermoregulatory enzyme stabilizer, phase splitting agent, phase stabilizing agent and thermo-conductive nanofluid, where the combination synergistically improves CO₂/H₂S loading and have a phase separation behaviour with energy-efficient regeneration for CO₂/H₂S.

Moreover, suitable combination of enzyme and solvent synergistically results in low corrosion, improved cyclic capacity and low viscosity alteration. The whole process is “stand alone” The possible advantages of the present inventions, but not limited to, are:

-   -   Efficient enzymatic phase transfer process.     -   Enzyme activation depends on temperature i.e. at low temperature         enzyme catalyze the absorption process whereas at higher         temperature, the same enzyme catalyses CO₂ desorption.     -   Fast phase separation improves the CO₂/H₂S separation         throughput.     -   Selective phase for CO₂ and H₂S observed, which resulted         selective regeneration of acid gases.     -   Low sensible heat requirement for solvent regeneration.

Objective:

An aim of the present invention is to provide a novel phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions.

Another objection of the present invention is to provide a process of preparing the phase transfer solvent composition of the present invention.

SUMMARY OF THE INVENTION

The invention provides a phase transfer solvent composed of a primary amine/secondary amine, a tertiary amine, a hyperthermophilic enzyme, thermoregulatory enzyme stabilizer, phase splitting agent, phase stabilizing agent and thermo-conductive fluid, where the combination synergistically improves CO₂/H₂S loading and exhibit a phase separation behavior with energy-efficient regeneration for CO₂/H₂S compared to conventional solvent systems. Further, the present invention provides a process of preparing the phase transfer solvent composition of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS

These and other features, aspects, and advantages of the present invention will become better understood when the following detailed description is read with reference to the accompanying drawings in which like characters represent like parts throughout the drawings wherein:

FIG. 1 illustrates Schematic representation of phase separation of solvent upon gas absorption.

FIG. 2 illustrates CO₂ loading in CO₂ lean and CO₂ rich phase with and without biocatalyst.

FIG. 3 illustrates flowchart of complete process for CO₂/H₂S capture using phase transfer solvent.

DETAILED DESCRIPTION

For the purpose of promoting an understanding of the principles of the invention, reference will now be made to the embodiments illustrated in the figures and specific language will be used to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended, such alterations and further modifications in the illustrated system, and such further applications of the principles of the invention as illustrated therein being contemplated as would normally occur to one skilled in the art to which the invention relates. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skilled in the art to which this invention belongs. The system, methods, and examples provided herein are illustrative only and not intended to be limiting.

The terminology and structure employed herein is for describing, teaching and illuminating some embodiments and their specific features and elements and does not limit, restrict or reduce the spirit and scope of the invention.

The invention discloses a novel phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions. More specifically, the disclosure relates to improved enzymatic and solvent systems, which upon CO₂/H₂S capture forms selective phases with higher CO₂/H₂S loading efficiency and low regeneration energy over the existing solvent systems. The disclosure further provides a phase transfer solvent composed of a primary amine/secondary amine, a tertiary amine, a hyperthermophilic enzyme, thermoregulatory enzyme stabilizer, phase splitting agent, phase stabilizing agent and thermo-conductive fluid, where the combination synergistically improves CO₂/H₂S loading and exhibit a phase separation behaviour with energy-efficient regeneration for CO₂/H₂S.

In an aspect of the present invention, inventors provide a phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions, comprising:

-   -   a) a compound having minimum one primary and/or one secondary         amine groups;     -   b) a compound having minimum one tertiary amine;     -   c) a hyperthermophilic enzyme;     -   d) a thermoregulatory enzyme stabilizer;     -   e) a phase splitting agent;     -   f) a phase stabilizing micellar agent;     -   g) a thermo-conductive fluid; and     -   h) 200-600 ml of demineralized water per litre to make up the         volume; wherein said solvent composition synergistically         improves CO₂/H₂S loading and exhibit a phase separation         behaviour with energy-efficient regeneration for CO₂/H₂S.

In an embodiment, said compound having minimum one primary and/or one secondary amine groups are selected from group consisting of Monoethanolamine, Diethanolamine, Triethanolamine, Monomethylethanolamine, 2-(2-aminoethoxy)ethanol, Aminoethylethanolamine, Ethylenediamine (EDA), Diethylenetriamine (DETA), Triethylenetetramine (TETA). Tetraethylenepentamine (TEPA), 2-amino 2methyl-1-proponal (AMP), 2-(ethyamino)-ethanol (EAE), 2-(methylamino)-ethanol (MAE), 2-(diethylamino)-ethanol (DEAE), diethanolamine (DEA), diisopropanolamine (DIPA), methylaminopropylamine (MAPA), 3-aminopropanol (AP), 2,2-dimethyl-1,3-propanediamine (DMPDA), 3-amino-1-cyclohexylaminopropane (ACHP), diglycola mine (DGA), 1-amino-2-propanol (MIPA), Isobutyl amine, 2-amino-2-methyl-ipropanol, 2-(2-aminoethylamino)ethanol, 2-amino-2-hydroxymethyl-i,3-propanediol, N-methyldiethanolamine, dimethylmonoethanolamine, diethylmonoethanolamine, triisopropanolamine and triethanolamine), trimethylamine, triethylamine, tripropylamine, tributylamine, dimethylethylamine, dimethylpropylamine, dimethylbutylamine, diethylmethylamine, diethylpropylamine, diethylbutylamine, N,N-diisopropylmethylamine, N-ethyldiisopropylamine, N,N-dimethyl ethyl amine, N,N-diethylbutylamine, 1,2-dimethylpropylamine, N,N-diethylmethylamine, N,N-dimethylisopropylamine, 1,3-dimethylbutylamine, 3,3-dimethylbutylamine, N,N-dimethylbutylamine, N-methyl-1,3-diaminopropane, Piperazine and triethylenetetramine or a combination thereof.

In another embodiment, said compound having minimum one primary and/or one secondary amine groups has a concentration range of 20-50 wt % in phase transfer solvent and depend on the feed gas CO₂ concentration.

In yet another embodiment, compounds having minimum one tertiary amine includes but not limited to diethylethanolamine, dimethylethanolamine, diisopropanolamine, methyldiethanolamine, triethanolamine, 2-Amino-2-MethylPropan-1-ol, bis (2-dimethylaminoethyl) ether, tetramethyl-1, 2-ethanediamine, tetramethyl-3-propane, N-methyl diethanolamine, Dimethylethanolamine Tetramethyl-6-hexanediamine , 1,3,5-Trimethylhexahydro-1,3,5-triazine N,N,N′,N′-Tetramethyl-2-butene-1,4-diamine, Pentamethyldipropylenetriamine, N,N-diethylethanolamine, N,N-dimethylbutylamine, 3-(methyloamino)propylamine, or a combination thereof.

In a further embodiment, compound having minimum one tertiary amine has a concentration range from 20-30 wt % in phase transfer solvent and depends on the feed gas CO₂ concentration.

In an embodiment, said hyperthermophilic enzyme is Carbonic Anhydrase (CA) obtained from a source selected from the group consisting of Bacillus thermoleovorans IOC-S3 (MTCC 25023) and/or Pseudomonas fragi IOC S2 (MTCC 25025), and/or Bacillus stearothermophilus IOC S1 (MTCC 25030) and/or Arthrobacter sp. IOC-SC-2 (MTCC 25028).

In another embodiment, said hyperthermophilic enzyme has concentration range of 10-50 ppm of the total phase transfer solvent.

In yet another embodiment, said thermoregulatory enzyme stabilizer is in the concentration range of 2-4 ppm per 1000 U/mg of enzyme.

In a further embodiment, said phase splitting agent is selected from sulfolane, tetrahydrothiophene-1-oxide, butadiene sulfone, and a combination thereof.

In an embodiment, said phase splitting agent has a concentration range from 1-5% in phase transfer solvent and depends on the tertiary amine concentration.

In another embodiment, said phase stabilizing micellar agent is selected from the group consisting of N-[2-[(2-Aminoethyl) amino]ethyl]-9-octadecenamide (AMEO), n-Benzalkonium chloride (BAC), C_(n)H_((2n+1))—COO(CH₂CH₂O)₁₂CH₃, Polyoxythylene alkyl ether, n-Alkyltrimethyl ammonium surfactant, Potassium alkanoate, Dodecylpyridinium bromide, Octylglucoside, Sodium dodecyl sulfate, trans-Cinnamaldehyde, Sodium bis-(2-ethylhexyl)-sulfosuccinate, Cetylpyridinium chloride, Primary alcohol ethoxylate, Polyoxyethylene nonyl phenyl ether, Polyethylene glycol esters, Linoleate, dodecylamine or a combination thereof.

In yet another embodiment, said phase stabilizing micellar agent has a concentration range from 50-70 ppm in phase transfer solvent.

In a further embodiment, said thermo-conductive fluid comprises nano-fluids of SiO₂, Al₂O₃, and TiO₂, Al₂O₃, TiCl₂/Nano-γ-Al₂O₃, CoFe₂O₄, magnetic Fe₃O₄, Ga₂O₃, functional silica, colloidal In₂O₃, ZnO, CoO, MnO₂, Fe₃O₄, PbS, MFe₂O₄ (M=Fe, Co, Mn, Zn), Lewis acid ZrO₂, silica boron sulfuric acid nanoparticles, Ni metal nanoparticles loaded on the acid-base bifunctional support (Al₂O₃), Co₃O₄ nanoparticles, oxide or metallic nano particle.

In an embodiment, said thermo-conductive fluid has a size in the range of between 10-50 nm and the concentration of the thermo-conductive fluid particle side ranges between 6-8 ppm.

In a second aspect of the present invention, the inventors provide a process of preparing the phase transfer solvent composition as claimed in claim 1, wherein said process comprises the steps of :

-   -   Step-1: Preparing modified hyperthermophilic enzyme;     -   Step-2: Preparing phase transfer solvent system; and     -   Step-3: Evaluating the obtained phase transfer solvent.

In an embodiment, said Step 1 comprises:

-   -   a) isolating hyperthermophilic enzyme from microbial strain         under suitable condition;     -   b) preparing thermoregulatory enzyme stabilizer using selective         oligonucleotide metal complex; and     -   c) complexing thermoregulatory enzyme stabilizer prepared in         step (b) with hyperthermophilic enzyme in step (a) to obtain the         modified hyperthermophilic enzyme.

In another embodiment, said condition for isolation of hyperthermophilic enzyme is as follows:

-   -   inducing enzyme expression by the addition of 0.5 mM ZnSO₄ in a         cell culture and growing the cells overnight at 55° C.;     -   lysing the cells by the use of a Bead-Beater and removing cell         debris by centrifugation;     -   pooling fractions containing the enzyme and dialyzing the same         against 0.1 M Tris/SO₄ at pH 7.5;     -   extracting the enzyme from the nutrient medium by 40% ammonium         sulfate precipitation;

wherein the extracted enzyme has concentration of 100-150 mg/ml with an p-NPA activity of 1800-2000 U/mg, able to be stored at −20° C. for two years without loss of activity, able to be stored at room temperature when immobilized can be stored for 1 year with 95-98% of initial activity and has a thermal stability of 100-110° C.

In yet another embodiment, the thermoregulatory enzyme stabilizer is prepared using metal complexation with selective oligonucleotide.

In a further embodiment, the oligonucleotide is a single stranded hexamer oligonucleotide with a minimum of two thiosine bases such as TTACTA, TTAATC, TTGATA, and TTGCTC or a combination thereof and the metal salt used for complexation is a chloride salt of Fe, Co, Cu and Ni or a combination thereof.

In an embodiment, the concentration of oligonucleotides and metal salts were of 5-10 pmol/μl and 50-100 pmol/μl, respectively for the synthesis of thermoregulatory enzyme stabilizer.

In another embodiment, complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme is due to hydrogen bonding.

In yet another embodiment, complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme is carried out by mixing 2 ppm of thermoregulatory enzyme stabilizer per 1000 U/mg of hyperthermophilic enzyme in presence of phosphate buffer (50 mM) of pH 6-6.5.

In a further embodiment, the activity of hyperthermophilic enzyme is enhanced after complexation with thermoregulatory enzyme stabilizer.

In an embodiment, complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme catalyses CO₂ absorption within a temperature range of 0-40° C.

In another embodiment, complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme catalyses CO₂ desorption in the temperature range of 50-110° C.

In yet another embodiment, the complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme can be used in free flow, fixed bed, rotating bed and any other configuration.

In a further embodiment, the complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme will be affective for phase transformation solvent, homogeneous solvent or any other form of solvent used for CO₂ capture.

In an embodiment, said Step 2 comprises:

-   -   a) preparing amine solution with compounds having minimum one         primary and/or one secondary amine groups by mixing said         solution for 1-2 hours;     -   b) adding compounds having at least one tertiary amine groups to         the above step (a) with constant stirring;     -   c) adding a phase splitting agent to the above step (b) and         mixing till formation of a homogeneous phase;     -   d) adding modified hyperthermophilic enzyme prepared in step-1 c         as defined in the present invention;     -   e) adding a phase stabilizing agent to the composition in the         above step (d);     -   f) after 2 hours of constant stirring of the mixture composition         obtained in the above step (e), adding a thermo-conductive fluid         to the same to obtain the final phase transfer solvent         composition which homogeneous at room temperature.

In another embodiment, said Step 3 comprises:

-   -   a) passing of CO₂/H₂S gas to the phase transfer solvent at         different condition;     -   b) allowing the separation of rich and lean CO₂/H₂S loading         phases;     -   c) separating the CO₂/H₂S lean phase and recycling the lean         phase into the absorber;     -   d) withdrawing the CO₂/H₂S rich stream and passing the same into         the stripper column for regeneration of the CO₂/H₂S;     -   e) After regeneration, allowing the CO₂/H₂S lean solvent stream         to the absorber;     -   f) measuring gas (CO₂/H₂S) loading in the solvent by gravimetric         method and pressure drop experiment;     -   g) determining the cyclic capacity;     -   h) monitoring viscosity after CO₂/H₂S loading for a period of         200 cycles and observing no change in viscosity;     -   i) monitoring corrosion for 0-100 days in a stainless vessel by         analysis the leaching metal ion in the solvent;     -   j) monitoring vapor pressure; and     -   k) conducting recyclability study of phase transfer solvent.

In yet another embodiment, the CO₂ concentration ranges from 0.02% to 99% , preferably 0.02% to 90% in the source gas and the H₂S concentration ranges from 0.001% to 5%.

In a further embodiment, the CO₂/H₂S phases differ in density, the rich phase is heavier than the CO₂/H₂S lean phase, allowing the phases to be separated by density, gravity or centrifugation apparatus.

In an embodiment, the separation of phases happens in 1-10 s for both CO₂ and H₂S gas feed.

In another embodiment, the CO₂ and H₂S rich phase is routed to different stripper column to selectively separate high pure H₂S and CO₂.

In yet another embodiment, the regeneration temperature ranges from 75° C. to 95° C.

In a further embodiment, CO₂ sources are carbon dioxide-containing flue gas, process gas or gas from bio-methanation.

In an embodiment, the resulting gas is passed through the solvent medium through in any suitable device forming the fine dispersion of gas which result in an increase in contact area, said gas is sparged in micro-bubble or nano-bubble size.

In another embodiment, the pressure of CO₂/H₂S ranges from ambient to 10 bar and temperature ranges between 20-50° C.

The following examples and experiments are for illustrative purposes only and not intended to limit the scope of this disclosure.

EXAMPLES

Material and Methods:

The typical concentration of components used in phase transfer solvent of the present invention are given in the following table-1

TABLE 1 Detail concentration of different components of phase transfer solvent Concentration in phase Component transfer solvent Compounds having minimum one primary 20-50 wt % and/or one secondary amine groups. Compounds having minimum one 20-30 wt % Tertiary amine Hyperthermophilic enzyme 10-50 ppm (1800-2000 U/mg) Thermoregulatory enzyme stabilizer 2-4 ppm per 1000 U/mg of enzyme Phase splitting agent 1-5 wt % Phase stabilizing micellar agent 50-70 ppm Thermo-conductive fluid 6-8 ppm DM water To make up the volume

Example 1: CO₂ Capture by Novel Phase Transfer Solvent

1. Preparation of Modified Hyperthermophilic Enzyme

The hyperthermophilic enzyme was extracted from Bacillus stearothermophilus IOC S1 (MTCC 25030). Initially, the microbes were grown in media having composition (in g/l) 6.0 g of Na₂HPO₄, 3.0 g of KH₂PO₄, 1.0 g of NH₄Cl, 0.5 g of NaCl, 0.014 g of CaCl₂, 0.245 g of MgSO₄.7H₂O, 10 mg of thiamine hydrochloride and 10 g of starch, and with 1 mM IPTG at 55° C. and 6.5 pH.

Enzyme expression was induced by the addition of 0.5 mM ZnSO₄ and the cells were grown overnight at 55° C. The cells were lysed by the use of a Bead-Beater and cell debris was removed by centrifugation. The pooled fractions containing the enzyme were dialyzed against 0.1 M Tris/SO₄ at pH 7.5. The enzyme was extracted from the nutrient medium by ammonium sulfate precipitation method. The purity of the enzyme was monitored by SDS/PAGE by comparing it with commercially available enzyme. The concentration of extracted enzyme was found to be 145 mg/ml by UV-Vis assay with p-NPA activity of 1955 U/mg. The enzyme was stored at RT.

For the preparation of thermoregulatory enzyme stabilizer, oligonucleotid of sequence TTACTA was synthesized. Oligonucleotides (100 mM oligonucleobases) and Iron chloride (100 mM) were prepared in HEPES buffer (10 mM, 1 mM magnesium nitrate, and pH 7.2).

Oligonucleotides and Iron chloride were then mixed with equal volumes. The final concentration of both oligonucleobases and iron chloride were both 50 mM. After equilibration at 30° C. for 10 minutes, the stable Fe-oligonucleotides complex was obtained and confirmed by appearance of sharp ligand to metal charge transfer spectra at 622 nm. The complex was collected by centrifugation with an rpm 8000 for 10 min.

2 ppm of thermoregulatory enzyme stabilizer was added to isolated hyperthermophilic enzyme (1L) having an activity of activity of 1955 U/mg. The solution was placed in the shaker overnight at 120 rpm at 60° C. resulting the modified hyperthermophilic enzyme. The characteristic of modified hyperthermophilic enzyme is given in table-2 Comparison of the activity for hyperthermophilic enzyme and modified hyperthermophilic enzyme using CO₂ or p-NPA as substrate is given in Table-2.

TABLE 2 Activity of biocatalyst before and after modification Biocatalyst Activity Hyperthermophilic enzyme 1955 U/mg Modified hyperthermophilic enzyme 3569 U/mg Hyperthermophilic enzyme@100° C. for 720 h 1912 U/mg Modified hyperthermophilic enzyme@100° C. for 720 h 3522 U/mg

2. Preparation of Phase Transfer Solvent System

In a 2L flask 5M diethylethanolamine and N,N-Dimethyl-1,3-diaminopropane (2M) were mixed for 2 h. To the solution 0.2M sulfolane was added drop-wise with 2 ml/min with constant stirring. To the same solution 50 ppm of modified hyperthermophilic enzyme was inserted followed by 70 ppm of phase stabilizing micellar agent (Sodium dodecyl sulfate). After 2 h of constant stirring 8 ppm of thermo-conductive fluid (Fe₂O₄ having average particle side 24 nm) was inserted to obtain the final phase transfer solvent system. The mixture is homogeneous at Room temperature.

3. Evaluation of Novel Phase Transfer Solvent

A known volume and mass (500 ml) of the solvent was weighed into the reactor and a synthetic mixture of CO₂ (35%) and balance N₂) was inserted to the solution, with a flow of 20 ml/min, was bubbled into the solvent. After bubbling through the solution, the gas stream was cooled on-line through two condensers placed on top of each other and the condensate was directly returned to the reactor. The purified gas was collected for GC analysis. The CO₂ loading was studied by gravimetric method under equilibrium condition. It was observed that upon CO₂ loading, the CO₂-rich phase formed in the bottom constitute 22% of the total solvent volume. The CO₂ rich phase was separated after used for desorption tests in stripping column.

TABLE 3 Table represents % of phase separation with respect to time. Time (s) CO₂ Lean phase (%) CO₂ Rich phase (%) 0 No Separation No Separation 2 68 32 5 71 29 10 78 22 20 78 22 100 79 21 500 79 21

4. CO₂ Loading Capacity in Rich and Lean Amine

FIG. 2 provides the comparative CO₂ loading in phase transfer solvent with and without biocatalyst. As shown in the figure, the biocatalyst significantly increase the CO₂ loading in CO₂ rich phase (6.31 mol/L) compared to that of rich solvent without biocatalyst (4.9 Mol/L).

TABLE 4 The time-dependent CO₂ uptake with various components of phase transfer solvents measured at 30° C. and 1 atm pressure using the gravimetric method. Observation of CO₂ loading phase separation Code Components (Mol/L) behaviors A Diethylethanolamine 2.3 No Phase separation B N,N-Dimethyl-1, 3- 1.1 No Phase diaminopropane separation C Dulfolane ND No Phase separation D Hyperthermophilic enzyme 0.04 No Phase separation E Thermoregulatory enzyme ND No Phase stabilizer-(Fe-TTACTA) separation F phase stabilizing micellar ND No Phase agent (Sodium dodecyl separation sulfate) G thermo-conductive fluid ND No Phase separation A + B 3.48 No Phase separation A + C 2.5 No Phase separation A + B + C 3.9 Phase separation A + B + D 4.2 No Phase separation A + B + E 3.45 No Phase separation A + B + F 3.42 No Phase separation A + B + C + D 4.9 Phase separation A + B + C + E 3.86 Phase separation A + B + C + F 1.91 Phase separation B + C + D + F 2.31 No Phase separation A + B + C + D + E + F + G 6.31 Phase separation (Novel phase transfer solvent)

TABLE 5 Desorption of CO₂ rich phase transfer solvent at 85-95° C. Phase transfer solvent Desorption (%) Phase transfer solvent-Without bio 68% catalyst phase transfer solvent-With 71% Hyperthermophilic enzyme phase transfer solvent-With 94% Modified Hyperthermophilic enzyme

TABLE 6 Cyclic capacity refers to the difference between lean and rich loading of a solvent. In this study, the lean loading was defined as CO₂ loading corresponding to CO₂ at equilibrium partial pressure of 0.05 kPa at 85-90° C. Lean Rich Cyclic loading loading capacity (mol CO₂/ (molCO₂/ (mol CO₂/ Solvent kg-solv) kg-solv) kg-solv) MEA 1.68 2.52 0.84 Phase transfer 0.07 6.3 6.23 solvent

Example-2: Biogas Purification by Phase Transfer Solvent

Preparation of Phase Transfer Solvent

The phase transfer solvent was prepared based on the protocol mentioned step-1,2 and 3 of the example-1.

Biogas of composition (75% Methane, 5000 ppm H₂S balance CO₂) was used for the study. The flow rate of solvent was kept 20 ml/min, was bubbled into the solvent. After bubbling through the solution, the gas stream was cooled on-line through two condensers placed on top of each other and the condensate was directly returned to the reactor. The purified gas was collected for GC analysis. The CO₂/H₂S loading was studied by gravimetric method under equilibrium condition. It was observed that upon CO₂ loading, the CO₂-rich phase formed in the bottom constitute 21.5% of the total solvent volume, H2S rich phase was 7% of the total volume. The CO₂ and H₂S rich phase were separated after used for desorption tests in stripping column.

TABLE 7 Table represents % of phase separation with respect to time. CO₂/H₂S Lean CO₂ Rich phase H₂S Rich phase Time (s) phase (%) (%) (%) 0 No Separation No Separation No Separation 2 62 29 9 5 65 28 7 10 71 22 7 20 71.5 22 6.5 100 72.5 21 6.5 500 72.5 21 6.5

TABLE 8 Effect of biocatalyst in CO₂ and H₂S loading CO₂ CO₂ H₂S H₂S loading in loading in loading in loading in rich phase rich phase rich phase rich phase (No (With (No (With Time biocatalyst) biocatalyst) biocatalyst) biocatalyst) 0 0 0 0 0 1 1.6 3.6 0.7 1.1 2 3.2 4.2 0.9 1.7 5 4.8 6.1 1.01 2.2 10 4.9 6.2 1.05 2.3 20 4.9 6.2 1.05 2.3 30 4.9 6.2 1.05 2.3

TABLE 9 Input Biogas Output methane Solvent system composition recovery Phase transfer CH₄ (50 V %) CH₄ (99.8 V %) solvent CO₂ (49.7 V %) CO₂ (0.2 V %) H₂S (3000 ppm) H₂S (N.D) CH₄ (60 V %) CH₄ (99.9 V %) CO₂ (39.6 V %) CO₂ (0.1 V %) H₂S (4000 ppm) H₂S (N.D) CH₄ (70 V %) CH₄ (99.9 V %) CO₂ (29.9 V %) CO₂ (0.1 V %) H₂S (1000 ppm) H₂S (N.D) CH₄ (80 V %) CH₄ (99.9 V %) CO₂ (19.5 V %) CO₂ (0.1 V %) H₂S (5000 ppm) H₂S (N.D)

It will thus be seen that the objects set forth above, among those made apparent from the preceding description, are efficiently attained, and since certain changes may be made in the constructions set forth without departing from the spirit and scope of the invention, it is intended that all matter contained in the above description shall be interpreted as illustrative and not in a limiting sense. The invention has been described with reference to preferred and alternate embodiments. Modifications and alterations will become apparent to those skilled in the art upon reading and understanding the detailed discussion of the invention provided herein. This invention is intended to include all such modifications and alterations insofar as they come within the scope of the present invention. These and other modifications of the preferred embodiments as well as other embodiments of the invention will be obvious from the disclosure herein, whereby the foregoing descriptive matter is to be interpreted merely as illustrative of the invention and not as a limitation.

Finally, to the extent necessary to understand or complete the disclosure of the present invention, all publications, patents, and patent applications mentioned herein are expressly incorporated by reference therein to the same extent as though each were individually so incorporated. 

1. A phase transfer solvent composition for enhanced CO₂ and/or H₂S capture from flue gas and biogas having various gaseous compositions, comprising: i) a compound having minimum one primary and/or one secondary amine groups; j) a compound having minimum one tertiary amine; k) a hyperthermophilic enzyme; l) a thermoregulatory enzyme stabilizer; m) a phase splitting agent; n) a phase stabilizing micellar agent; o) a thermo-conductive fluid; and p) 200-600 ml of demineralized water/litre to make up the volume; wherein said solvent composition synergistically improves CO₂/H₂S loading and exhibit a phase separation behaviour with energy-efficient regeneration for CO₂/H₂S.
 2. The phase transfer solvent composition as claimed in claim 1, wherein said compound having minimum one primary and/or one secondary amine groups are selected from group consisting of Monoethanolamine, Diethanolamine, Triethanolamine, Monomethylethanolamine, 2-(2-aminoethoxy)ethanol, Aminoethylethanolamine, Ethylenediamine (EDA), Diethylenetriamine (DETA), Triethylenetetramine (TETA). Tetraethylenepentamine (TEPA), 2-amino 2methyl-1-proponal (AMP), 2-(ethyamino)-ethanol (EAE), 2-(methylamino)-ethanol (MAE), 2-(diethylamino)-ethanol (DEAE), diethanolamine (DEA), diispropanolamine (DIPA), methylaminopropylamine (MAPA), 3-aminopropanol (AP), 2,2-dimethyl-1,3-propanediamine (DMPDA), 3-amino-1-cyclohexylaminopropane (ACHP), diglycola mine (DGA), 1-amino-2-propanol (MIPA), Isobutyl amine, 2-amino-2-methyl-ipropanol, 2-(2-aminoethylamino)ethanol, 2-amino-2-hydroxymethyl-i,3-propanediol, N-methyldiethanolamine, dimethylmonoethanolamine, diethylmonoethanolamine, triisopropanolamine and triethanolamine), trimethylamine, triethylamine, tripropylamine, tributylamine, dimethylethylamine, dimethylpropylamine, dimethylbutylamine, diethylmethylamine, diethylpropylamine, diethylbutylamine, N,N-diisopropylmethylamine, N-ethyldiisopropylamine, N,N-dimethylethylamine, N,N-diethylbutylamine, 1,2-dimethylpropylamine, N,N-diethylmethylamine, N,N-dimethylisopropylamine, 1,3-dimethylbutylamine, 3,3-dimethylbutylamine, N,N-dimethylbutylamine, N-methyl-1,3-diaminopropane, Piperazine and triethylenetetramine or a combination thereof; wherein said compound having minimum one primary and/or one secondary amine groups has a concentration range of 20-50 wt % in phase transfer solvent and depend on the feed gas CO₂ concentration.
 3. The phase transfer solvent composition as claimed in claim 1, wherein compounds having minimum one tertiary amine are selected from diethylethanolamine, dimethylethanolamine, diisopropanolamine, methyldiethanolamine, triethanolamine, 2-Amino-2-MethylPropan-1-ol, bis (2-dimethylaminoethyl) ether, tetramethyl-1,2-ethanediamine, tetramethyl-3-propane, N-methyl diethanolamine, Dimethylethanolamine Tetramethyl-6-hexanediamine, 1,3,5-Trimethylhexahydro-1,3,5-triazine N,N,N′,N′-Tetramethyl-2-butene-1,4-diamine, Pentamethyldipropylenetriamine, N,N-diethylethanolamine, N,N-dimethylbutylamine, 3-(methyloamino)propylamine, or a combination thereof; and wherein compound having minimum one tertiary amine has a concentration range from 20-30 wt % in phase transfer solvent and depends on the feed gas CO₂ concentration.
 4. The phase transfer solvent composition as claimed in claim 1, wherein said hyperthermophilic enzyme is Carbonic Anhydrase (CA) obtained from a source selected from the group consisting of Bacillus thermoleovorans IOC-S3 (MTCC 25023) and/or Pseudomonas fragi IOC S2 (MTCC 25025), and/or Bacillus stearothermophilus IOC S1 (MTCC 25030) and/or Arthrobacter sp. IOC-SC-2 (MTCC 25028); and wherein said hyperthermophilic enzyme has concentration range of 10-50 ppm of the total phase transfer solvent; and wherein said thermoregulatory enzyme stabilizer is in the concentration range of 2-4 ppm per 1000 U/mg of enzyme.
 5. The phase transfer solvent composition as claimed in claim 1, wherein said phase splitting agent is selected from sulfolane, tetrahydrothiophene-1-oxide, butadiene sulfone, and a combination thereof, wherein said phase splitting agent has a concentration range from 1-5% in phase transfer solvent and depends on the tertiary amine concentration.
 6. The phase transfer solvent composition as claimed in claim 1, wherein said thermo-conductive fluid comprises nano-fluids of SiO₂, Al₂O₃, and TiO₂, Al₂O₃, TiCl₂/Nano-γ-Al₂O₃, CoFe₂O₄, magnetic Fe₃O₄, Ga₂O₃, functional silica, colloidal In₂O₃, ZnO, CoO, MnO₂, Fe₃O₄, PbS, MFe₂O₄ (M=Fe, Co, Mn, Zn), Lewis acid ZrO₂, silica boron sulfuric acid nanoparticles, Ni metal nanoparticles loaded on the acid-base bifunctional support (Al₂O₃), Co₃O₄ nanoparticles, oxide or metallic nano particle; and wherein said thermo-conductive fluid has a size in the range of between 10-50 nm and the concentration of the thermo-conductive fluid particle side ranges between 6-8 ppm.
 7. The phase transfer solvent composition as claimed in claim 1, wherein said phase stabilizing micellar agent is selected from the group consisting of N-[2-[(2-Aminoethyl) amino]ethyl]-9-octadecenamide (AMEO), n-Benzalkonium chloride (BAC), C_(n)H_((2n+1))—COO(CH₂CH₂O)₁₂CH₃, Polyoxythylene alkyl ether, n-Alkyltrimethyl ammonium surfactant, Potassium alkanoate, Dodecylpyridinium bromide, Octylglucoside, Sodium dodecyl sulfate, trans-Cinnamaldehyde, Sodium bis-(2-ethylhexyl)-sulfosuccinate, Cetylpyridinium chloride, Primary alcohol ethoxylate, Polyoxyethylene nonyl phenyl ether, Polyethylene glycol esters, Linoleate, dodecylamine or a combination thereof and wherein said phase stabilizing micellar agent has a concentration range from 50-70 ppm in phase transfer solvent.
 8. A process of preparing the phase transfer solvent composition as claimed in claim 1, wherein said process comprises the steps of: Step-1: Preparing modified hyperthermophilic enzyme, wherein said step comprises; a) isolating hyperthermophilic enzyme from microbial strain under suitable condition; b) preparing thermoregulatory enzyme stabilizer using selective oligonucleotide metal complex, wherein selective oligonucleotide is a single stranded hexamer oligonucleotide with a minimum of two thiosine bases such as TTACTA, TTAATC, TTGATA, and TTGCTC or a combination thereof and the metal salt used for complexation is a chloride salt of Fe, Co, Cu and Ni or a combination thereof and wherein the concentration of oligonucleotides and metal salts were of 5-10 pmol/μl and 50-100 pmol/μl, respectively for the synthesis of thermoregulatory enzyme stabilize; and c) complexing thermoregulatory enzyme stabilizer prepared in step (b) with hyperthermophilic enzyme in step (a) to obtain the modified hyperthermophilic enzyme, wherein complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme is due to hydrogen bonding and is carried out by mixing 2 ppm of thermoregulatory enzyme stabilizer per 1000 U/mg of hyperthermophilic enzyme in presence of phosphate buffer (50 mM) of pH 6-6.5 resulting increase in the activity of hyperthermophilic enzyme; Step-2: Preparing phase transfer solvent system, wherein said Step 2 comprises: a) preparing amine solution with compounds having minimum one primary and/or one secondary amine groups by mixing said solution for 1-2 hours; b) adding compounds having at least one tertiary amine groups to the above step (a) with constant stirring; c) adding a phase splitting agent to the above step (b) and mixing till formation of a homogeneous phase; d) adding modified hyperthermophilic enzyme prepared in step-1 c as defined in claims 16-23; e) adding a phase stabilizing agent to the composition in the above step (d); f) after 2 hours of constant stirring of the mixture composition obtained in the above step (e), adding a thermo-conductive fluid to the same to obtain the final phase transfer solvent composition which homogeneous at room temperature; and Step-3: Evaluating the obtained phase transfer solvent, said Step 3 comprises: a) passing of CO₂/H₂S gas to the phase transfer solvent at different condition; b) allowing the separation of rich and lean CO₂/H₂S loading phases; c) separating the CO₂/H₂S lean phase and recycling the lean phase into the absorber; d) withdrawing the CO₂/H₂S rich stream and passing the same into the stripper column for regeneration of the CO₂/H₂S; wherein the regeneration temperature ranges from 75° C. to 95° C.; e) After regeneration, allowing the CO₂/H₂S lean solvent stream to the absorber; f) measuring gas (CO₂/H₂S) loading in the solvent by gravimetric method and pressure drop experiment; g) determining the cyclic capacity; h) monitoring viscosity after CO₂/H₂S loading for a period of 200 cycles and observing no change in viscosity; i) monitoring corrosion for 0-100 days in a stainless vessel by analysis the leaching metal ion in the solvent; j) monitoring vapor pressure; wherein the pressure of CO₂/H₂S ranges from ambient to 10 bar and temperature ranges between 20-50° C.; and k) conducting recyclability study of phase transfer solvent.
 9. The process of preparing the phase transfer solvent composition as claimed in claim 8, wherein said condition for isolation of hyperthermophilic enzyme is as follows: inducing enzyme expression by the addition of 0.5 mM ZnSO₄ in a cell culture and growing the cells overnight at 55° C.; lysing the cells by the use of a Bead-Beater and removing cell debris by centrifugation; pooling fractions containing the enzyme and dialyzing the same against 0.1 M Tris/SO₄ at pH 7.5; extracting the enzyme from the nutrient medium by 40% ammonium sulfate precipitation; wherein the extracted enzyme has concentration of 100-150 mg/ml with an p-NPA activity of 1800-2000 U/mg , able to be stored at −20° C. for two years without loss of activity, able to be stored at room temperature when immobilized can be stored for 1 year with 95-98% of initial activity, and has a thermal stability of 100-110° C.
 10. The process of preparing the phase transfer solvent composition as claimed in claim 8, wherein complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme catalyses CO₂ absorption within a temperature range of 0-40° C., preferably 50-110° C.; complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme can be used in free flow, fixed bed, rotating bed and any other configuration; and complexation of thermoregulatory enzyme stabilizer and hyperthermophilic enzyme will be affective for phase transformation solvent, homogeneous solvent or any other form of solvent used for CO₂ capture.
 11. The process as claimed in claim 8, wherein said compound having minimum one primary and/or one secondary amine groups are selected from group consisting of Monoethanolamine, Diethanolamine, Triethanolamine, Monomethylethanolamine, 2-(2-aminoethoxy)ethanol, Aminoethylethanol amine, Ethylenediamine (EDA), Diethylenetriamine (DETA), Triethylenetetramine (TETA). Tetraethyl enepentamine (TEPA), 2-amino 2methyl-1-proponal (AMP), 2-(ethyamino)-ethanol (EAE), 2-(methylamino)-ethanol (MAE), 2-(diethylamino)-ethanol (DEAE), diethanolamine (DEA), diisopropanolamine (DIPA), methylaminopropylamine (MAPA), 3-aminopropanol (AP), 2,2-dimethyl-1,3-propanediamine (DMPDA), 3-amino-1-cyclohexylaminopropane (ACHP), diglycola mine (DGA), 1-amino-2-propanol (MIPA), Isobutyl amine, 2-amino-2-methyl-ipropanol, 2-(2-aminoethylamino)ethanol, 2-amino-2-hydroxymethyl-i,3-propanediol, N-methyldiethanolamine, dimethylmonoethanolamine, diethylmonoethanolamine, triisopropanolamine and triethanolamine), trimethylamine, triethylamine, tripropylamine, tributylamine, dimethylethylamine, dimethylpropylamine, dimethylbutylamine, diethylmethylamine, diethylpropylamine, diethylbutylamine, N,N-diisopropylmethylamine, N-ethyldiisopropylamine, N,N-dimethylethylamine, N,N-diethylbutylamine, 1,2-dimethylpropylamine, N,N-diethylmethylamine, N,N-dimethylisopropylamine, 1,3-dimethylbutylamine, 3,3-dimethylbutylamine, N,N-dimethylbutylamine, N-methyl-1,3-diaminopropane ,Piperazine and triethylenetetramine or a combination thereof; wherein said compound having minimum one primary and/or one secondary amine groups has a concentration range of 20-50 wt % in phase transfer solvent and depend on the feed gas CO₂ concentration.
 12. The process as claimed in claim 8, wherein compounds having minimum one tertiary amine are selected from diethylethanolamine, dimethylethanolamine, diisopropanolamine, methyldiethanolamine, triethanolamine, 2-Amino-2-MethylPropan-1-ol, bis (2-dimethylaminoethyl) ether, tetramethyl-1, 2-ethanediamine, tetramethyl-3-propane, N-methyl diethanolamine, Dimethylethanolamine Tetramethyl-6-hexanediamine, 1,3,5-Trimethylhexahydro-1,3,5-triazine N,N,N′,N′-Tetramethyl-2-butene-1,4-diamine, Pentamethyldipropylenetriamine, N,N-diethylethanolamine, N,N-dimethylbutylamine, 3-(methyloamino)propylamine, or a combination thereof; and wherein compound having minimum one tertiary amine has a concentration range from 20-30 wt % in phase transfer solvent and depends on the feed gas CO₂ concentration.
 13. The process as claimed in claim 8, wherein said hyperthermophilic enzyme is Carbonic Anhydrase (CA) obtained from a source selected from the group consisting of Bacillus thermoleovorans IOC-S3 (MTCC 25023) and/or Pseudomonas fragi IOC S2 (MTCC 25025), and/or Bacillus stearothermophilus IOC S1 (MTCC 25030) and/or Arthrobacter sp. IOC-SC-2 (MTCC 25028); and wherein said hyperthermophilic enzyme has concentration range of 10-50 ppm of the total phase transfer solvent; and wherein said thermoregulatory enzyme stabilizer is in the concentration range of 2-4 ppm per 1000 U/mg of enzyme.
 14. The process as claimed in claim 8, wherein said phase splitting agent is selected from sulfolane, tetrahydrothiophene-1-oxide, butadiene sulfone, and a combination thereof, wherein said phase splitting agent has a concentration range from 1-5% in phase transfer solvent and depends on the tertiary amine concentration.
 15. The process as claimed in claim 8, wherein said thermo-conductive fluid comprises nano-fluids of SiO₂, Al₂O₃, and TiO₂, Al₂O₃, TiCl₂/Nano-γ-Al₂O₃, CoFe₂O₄, magnetic Fe₃O₄, Ga₂O₃, functional silica, colloidal In₂O₃, ZnO, CoO, MnO₂, Fe₃O₄, PbS, MFe₂O₄ (M=Fe, Co, Mn, Zn), Lewis acid ZrO₂, silica boron sulfuric acid nanoparticles, Ni metal nanoparticles loaded on the acid-base bifunctional support (Al₂O₃), Co₃O₄ nanoparticles, oxide or metallic nano particle; and wherein said thermo-conductive fluid has a size in the range of between 10-50 nm and the concentration of the thermo-conductive fluid particle side ranges between 6-8 ppm.
 16. The process of preparing the phase transfer solvent composition as claimed in claim 8, wherein the CO₂ concentration ranges from 0.02% to 99%, preferably 0.02% to 90% in the source gas and the H₂S concentration ranges from 0.001% to 5%; CO₂/H₂S phases differ in density, the rich phase is heavier than the CO₂/H₂S lean phase, allowing the phases to be separated by density, gravity or centrifugation apparatus; wherein the separation of phases happens in 1-10 s for both CO₂ and H₂S gas feed.
 17. The process of preparing the phase transfer solvent composition as claimed in claim 9, wherein the CO₂ and H₂S rich phase is routed to different stripper column to selectively separate high pure H₂S and CO₂.
 18. The process of preparing the phase transfer solvent composition as claimed in claim 8, wherein CO₂ sources are carbon dioxide-containing flue gas, process gas or gas from bio-methanation.
 19. The process of preparing the phase transfer solvent composition as claimed in claim 8, wherein, the resulting gas is passed through the solvent medium through in any suitable device forming the fine dispersion of gas which result in an increase in contact area, said gas is sparged in micro-bubble or nano-bubble size. 